Periodic regeneration of a deactivated solid alkylation catalyst with hydrogen

Abstract: Deactivated solid catalytic composites of the reaction product of a metal halide having Friedel-Crafts activity with the bound surface hydroxyl group of inorganic oxides and containing a zerovalent metal with hydrogenation activity, used as a catalyst in motor fuel until deactivated, is regenerated by treating the composite after alkylate feedstock has been removed with hydrogen at regeneration conditions including a temperature in the range of 10 to 300°C. Multiple regenerations are possible without appreciable activity loss.

Description: BACKGROUND OF THE INVENTION Even in the era of anti-knock additives such as tetraethyl lead, the use of alkylate as a component in motor fuel gained both universal acceptance and importance. In the ensuing years alkylate has become an even more important component of motor fuel. Alkylate is an economical, clean-burning, high-octane, low volatility product that is becoming increasingly important as the composition of gasoline changes in response to environmental concerns and legislation in some parts of the world. These governmental regulations most applicable to the increasing importance of alkylates are those affecting lead and butane. Adding lead anti-knock compounds was the easiest way to raise gasoline octane, but because of continuing concerns over the effects of lead emissions the phasing out of lead in gasoline was required, a process over 90% complete in the U.S. Butane is another effective octane-booster but tends to evaporate from gasoline, especially in warm weather, contributing to smog formation. Recent regulations in the U.S. have effected their virtually complete removal from gasoline. The term "alkylate" generally refers to a complex mixture resulting from the alkylation of olefins present or formed in a feedstream of C2-C6 olefins with intermediates arising primarily from alkanes, especially branched alkanes, and predominantly those with 4 carbon atoms, especially isobutane, also present in the same feedstream. It is most desirable that the complex product mixture referred to as alkylate contains predominantly trimethylpentanes, since these are high-octane components which add considerable value to motor fuel, yet the chemistry of alkylation affords a dazzling variety of products resulting from only a few basic chemical reactions characteristic of the carbonium ion which plays a central role in the alkylation process. Thus, chain transfer (intermolecular hydride transfer and alkyl shifts), oligomerization and disproportionation serve to place into the alkylate as byproduct materials of from 5-12+ carbon atoms from a feed containing only C4 olefins and alkanes. The alkylation of olefins is catalyzed by strong acids generally. Although such alkylation has been the focus of intense and continuing scrutiny for several decades, the requirements of optimum selectivity while achieving high conversion have heretofore narrowed, for all practical purposes, the commercial choice of catalyst to sulfuric acid and liquid hydrogen fluoride. While processes based on each of these acids have gained commercial acceptance those based on HF have been favored at least in part because of the relative ease of HF regeneration. A brief but valuable overview of HF-catalyzed alkylation is presented by B.R. Shah in "Handbook of Petroleum Refining Processes", R.A. Meyers, editor, McGraw-Hill Book Company, 1986, pp 1-3 through 1-28. In a rather over-simplified description, the HF-catalyzed alkylation process is carried out as follows. Olefinic and isobutane feedstocks are combined and mixed with HF in an alkylation reaction zone. The reactor effluent is separated into the desired alkylate, acid, and other light gases which are predominantly unreacted isobutanes. The HF is either recycled to the reactor directly or regenerated, in whole or in part, prior to its being recycled to the reactor. Unreacted isobutane also is recycled to the reactor, and the alkylate is then used in motor fuel blending. Recently HF (hydrofluoric acid) has come under environmental pressure in the U.S. Hydrofluoric add is classified as an Acutely Hazardous Material, and in Southern California the Board of the South Coast Air Quality Management District recently required that the use of HF in alkylation be phased out by January 1, 1998. This phase out is expected to be a worldwide trend. Consequently there is increasing reason to seek substitutes for HF as an alkylation catalyst for alkylate production. It is quite desirable to have a solid acid as an effective catalyst, for this permits development of fixed bed processes, a desirable alternative in the petroleum refining industry. One of the promising solid catalysts for alkylation of C2-C6 olefins with alkanes in the 4 to 6 carbon range, a process hereafter specifically referred to as motor fuel alkylation, is the reaction product between one or more of the metal halides active as Friedel-Crafts catalysts and a refractory inorganic oxide having surface hydroxyl groups, where the refractory inorganic oxide also contains dispersed thereon a metal having hydrogenation activity for olefins. Such catalysts are reasonably well known in the art, as exemplified by US-A-2999074, and includes, for example, the reaction product of aluminum chloride and alumina containing zerovalent platinum. As is commonly the case, these catalysts deactivate with use, where the deactivation is measured by the percent conversion of olefins, and it is imperative to have means of repeatedly regenerating these catalysts, i.e., to restore their activity, in order to utilize their catalytic effectiveness over long periods of time. It is further desirable that the method of regeneration be minimally disruptive to the motor fuel alkylation process itself. By that is meant that it is most desirable that the catalyst not be subjected to conditions or agents foreign to those of the alkylation process itself. It is still further desirable to minimize the regeneration cycle time relative to the alkylation cycle time. That is, if the complete process cycle time be the sum of the time during which the catalyst is used in alkylation (alkylation cycle time) and the time during which the catalyst is regenerated (regeneration cycle time) one desires that the latter be as short as possible. Of course the ideal regeneration cycle time is zero, but this corresponds to the case where the catalyst does not deactivate which, unfortunately, is contrary to experience. A simple yet effective method of regenerating a deactivated catalyst has now been found which satisfies both of the foregoing criteria. More particularly, it is found that after removing liquid hydrocarbons from the deactivated catalyst, treatment of the catalyst with hydrogen at approximately the same pressure as that used during alkylation and at reasonably low temperatures affords virtually complete regeneration, often with increased product quality. This method is simple, very effective both in restoring activity and affording multiple regenerations, and requires a cycle time which is commercially feasible. US-A-4098833 relates to regeneration of a catalyst of a metal halide and a Bronsted acid containing fluorine, where the deactivated catalyst may have been used as an alkylation catalyst, using hydrogen and a separate noble metal hydrogenation component. The patentee's catalyst is different from that used in the present invention in many respects, including the fact that his catalyst is unsupported, is liquid, and always includes a fluorine-containing Bronsted acid. US-A-3352941 and US-A-3318820 describe regeneration of a hydrocarbon-conversion catalyst, more especially an isomerization catalyst consisting essentially of the reaction product of aluminum halide and hydroxyl groups of surface-hydroxyl-containing adsorbent solid, such as alumina and silica, by treatment with hydrogen, followed in the case of US-A-3318820 by treatment with gaseous HCl. No noble metal hydrogenation component is mentioned, and post-hydrogen treatment with HCl is an essential part of the regeneration process of US-A-3318820. The purpose of the present invention is to repeatedly restore the activity of a solid catalyst of metal halides reacted with surface hydroxyl groups of refractory inorganic oxides and which also contain small amounts of a metal active in hydrogenation where such catalysts have become deactivated in use as a motor fuel liquid phase alkylation catalyst. More specifically, the present invention provides a method of regenerating an at least partially deactivated solid catalyst comprising 1) the reaction product of a first metal halide and the bound surface hydroxyl groups of refractory inorganic oxide by treatment with hydrogen and recovering a regenerated catalyst having substantially increased alkylation activity wherein the catalyst is an alkylation catalyst containing said reaction product (1), and 2) a zerovalent second metal, wherein said first metal halide is a fluoride, chloride, or bromide and the first metal is selected from aluminum, zirconium, tin, tantalum, titanium, gallium, antimony, phosphorus, boron and mixtures thereof, and said zerovalent second metal is selected from platinum, palladium, nickel, ruthenium, rhodium, osmium, iridium, and mixtures thereof, said catalyst having become at least partially deactivated during its catalysis of the liquid phase alkylation of an alkene having from 2 to 6 carbon atoms with an alkane having from 4 to 6 carbon atoms, said method comprising removing substantially all of the liquid phase hydrocarbons from the catalyst, and treating the resulting catalyst with hydrogen in the presence of liquid isobutane and a chloride source at a partial pressure of 6.9 to 13790 kPa for a time from 1 up to 20 hours at a temperature from 10 up to 300°C. In a more specific embodiment the refractory inorganic oxide is alumina. In another specific embodiment the metal halide is aluminum chloride. In a still more specific embodiment the metal halide is aluminum chloride, the refractory inorganic oxide is alumina, and the metal having hydrogenation activity is platinum. Although the group of catalysts which may be characterized as the reaction products of a Friedel-Crafts active metal halide and surface hydroxyl groups of inorganic oxides and which additionally contain a zerovalent metal having hydrogenation activity show promise in the liquid phase alkylation of alkenes with alkanes to produce alkylates valuable as a component of motor fuel, such catalysts deactivate quickly. Therefore there is a need to develop a method of regenerating the catalyst, preferably by procedures which are relatively simple, which are inexpensive, and which are effective in restoring catalytic activity over many multiple regeneration cycles. This application describes such a method, which is to substantially free the catalyst of the liquid phase reaction mixture and then treat the catalysts with hydrogen at temperatures of at least 10°C up to about 300°C and at a hydrogen partial pressure at least 6.9 to 13790 kPa. Treatment of the catalyst with hydrogen is effected in the presence of liquid isobutane and a chloride source. Because the catalysts used in this invention are well known in the art (see US-A-2999074 and US-A-3318820) it is not necessary to describe them here at great length, accordingly the following description will merely suffice to afford the reader an understanding of our invention. The refractory inorganic oxides suitable for use in this invention have a surface area of at least 35 m 2 /g, preferably greater than 50 m 2 /g, and more desirably greater than 100 m 2 /g. There appears to be some advantage to working with materials having as high a surface area as possible, although some exceptions also are known. Suitable refractory inorganic oxides include alumina, titania, zirconia, chromia, silica, boria, silica-alumina, aluminum phosphate, and combinations thereof. Of these alumina is particularly preferred. Any alumina phase may be used so long as it has a surface area of at least 35 m 2 /g and has surface hydroxyl groups, which for all practical matters excludes alpha-alumina, although the various phases are not necessarily equivalent in their effectiveness as a motor fuel alkylation catalyst. It is required that the refractory inorganic oxide have surface hydroxyl groups, by which is meant not adsorbed water but rather hydroxyl (OH) groups whose oxygen is bound to the metal of the inorganic oxide. These latter hydroxyl groups sometimes have been referred to as chemically combined hydroxyl. Since the presence of adsorbed water is generally detrimental to the preparation of the catalysts of our invention, the refractory inorganic oxides are first treated to remove surface hydroxyl groups from water, most usually by calcination at a temperature which specifically and preferentially removes physically adsorbed water without chemically altering the other hydroxyl groups. For example, temperatures ranging from 350°C to 700°C are usually satisfactory where the inorganic oxide is alumina. A zerovalent metal having hydrogenation activity generally is deposited on the refractory inorganic oxide prior to the reaction of its surface hydroxyl groups with metal halides. Although such a procedure has proven both convenient and effective, this is not the only sequence which may be used to afford an effective catalyst. Metals which have been found to be particularly effective include nickel and the noble metals of platinum, palladium, ruthenium, rhodium, osmium, and iridium, although platinum and palladium are by far the most desirable of the noble metals. The desired metal may be composited with the refractory inorganic oxide in any desired manner, such as by impregnation, coprecipitation, dipping, and so forth. Such methods are well known and need not be described here. Metal levels may range between about 0.01 up to about 1.0 weight percent for the noble metals, based on the weight of the finished catalyst, and from about 0.1 up to about 5 weight percent for nickel. The composite of the metal and refractory inorganic oxide is dried and calcined under controlled conditions to remove physically adsorbed water but under sufficiently mild conditions so that the "chemically combined" hydroxyl groups are not eliminated. Subsequent to metal deposition and calcination, the surface hydroxyl groups of the refractory inorganic oxide are reacted with a metal halide having Friedel-Crafts activity. Among the metals which may be used are included aluminum, zirconium, tin, tantalum, titanium, gallium, antimony, phosphorous, and boron. Suitable halides are the fluorides, chlorides, and bromides. Representative of such metal halides include aluminum chloride, aluminum bromide, ferric chloride, ferric bromide, zirconium chloride, zirconium bromide, boron trifluoride, titanium tetrachloride, gallium chloride, tin tetrachloride, antimony fluoride, tantalum chloride, tantalum fluoride, phosphorus chloride, phosphorus fluoride, and so forth. Of these metal halides the aluminum halides are preferred, especially aluminum chloride. Except for boron trifluoride, the chlorides are generally the preferable halides. The reaction between the metal halides of this invention and the surface hydroxyl groups of the refractory inorganic oxide is readily accomplished by, for example, sublimation or distillation of the metal halide onto the surface of the particles of the metal-inorganic oxide composite. The reaction is attended by the elimination of between about 0.5 and 2.0 moles of hydrogen halide per mole of metal halide adsorbed thereon. The reaction temperature will depend upon such variables as the reactivity of metal halides and its sublimation temperature or boiling point, where the metal halide is reacted in the gas phase, as well as on the nature of the refractory inorganic oxide. For example, using aluminum chloride and alumina as our specific examples reaction readily occurs within the range between about 190 through 600°C. The following method has been found to be very effective in restoring lost activity to such a catalyst and to be effective over many regeneration cycles. It is first necessary to remove substantially all of the liquid reaction mixture from the catalyst, which can be done quite simply by draining all of the liquid phase from the catalyst. After the liquid phase is removed the catalyst is treated with hydrogen at a partial pressure between about 6.9 to 13790 kPa (1 up to 2,000 psi). The temperature at which the catalyst is treated with hydrogen varies between 10 and 300°C. Regeneration time depends inversely with temperature. Consequently, higher temperatures are favored if a shorter regeneration time is desirable, and for this reason temperatures even higher than 300°C may be used although these are not generally recommended. Times of 1 to 20 hours are generally sufficient. However, other factors favor low temperatures regeneration. Regeneration at alkylation process conditions is most desirable in order to eliminate the costs of heating and cooling, and to make regeneration operationally simpler and easier. In fact, regeneration is preferably done in the temperature range between about 10 and about 200°C, for which a regeneration time on the order of 6 hours suffices to effect maximum restoration of activity. The following examples are illustrative of the invention. General Procedure . Typical alkylation test conditions included a temperature of 10°C, a reaction pressure of 3200 kPa (450 psig), a butene-2 LHSV of 0.2 hr -1 with an isobutane/butene mole ratio of 100, 75, 45, or 20. Alkylation was performed in the presence of 2,000 ppm chloride (as butyl chloride) and with hydrogen present at 0.25 mole proportions relative to butene. Catalyst regeneration with hydrogen was performed as follows. At the end of a process cycle (i.e., when catalyst had appreciably deactivated) a stream of isobutane was introduced at 1 LHSV and the isobutane/olefin feedstock was cut out. After two hours of flushing at 10°C, the system was depressurized to 101 kPa (1 atmosphere), after which hydrogen was introduced along with 10-1000 ppm of chloride as butyl chloride and the system pressurized to 3200 kPa (450 psig). The temperature was raised to 200°C and maintained at that temperature for 4 hours, after which the reactor was cooled to 10°C over approximately 2 hours and then filled and flushed with isobutane for an additional 1-2 hours. The entire procedure lasted approximately 10 hours. EXAMPLE 1 (COMPARISON) Regeneration with pure hydrogen . A catalyst was prepared containing 0.25 weight percent platinum on 1.6 mm (1/16") gamma alumina extrudates on which had been sublimed aluminum chloride in an amount corresponding to 0.75 weight percent Al. (Aluminum content was not measured directly, but rather was determined on the basis of chloride content.) The catalyst then was treated with a chloride source so that it initially contained chloride in the range of 3-7 weight percent, where suitable chloride sources include an alkyl chloride or hydrogen chloride. This catalyst was used in motor fuel alkylation under the conditions stated above and regenerated as described above for 10 process cycles. There was no observable activity loss between cycles 2 and 10, all of which were conducted at an isobutane/butene ratio of 45. The average alkylate product calculated research octane number (RON) was about 89 for all cycles. A control was run using the same catalyst except without platinum. No regeneration was observed; the catalyst alter hydrogen treatment continued to deactivate unabated without any measurable restoration of activity. Similar experiments were conducted using gallium chloride, GaCl 3 , in place of aluminum chloride. Although regeneration tests were not so extensive the deactivated catalyst was completely regenerated under the conditions described above. The product alkylate showed an RON of 90.5. In another run palladium at 0.5 weight percent replaced the platinum in an aluminum chloride-alumina catalyst. The regeneration was successfully performed and the average alkylate product RON was about 88.5. EXAMPLE 2 Regeneration with isobutane, butyl chloride, and hydrogen . Because chloride loss is observed from catalysts when regeneration is done in an isobutane-hydrogen stream with subsequent deactivation of the catalyst, it is highly desirable to perform the regeneration in the presence of an organic chloride, such as butyl chloride. In these regenerations isobutane containing 1,000 ppm chloride (as butyl chloride) and hydrogen cofed at 0.0283 m 3 /hr (1 standard cubic foot an hour) were cut in at the end of the process cycle at the same time that feed blend was cut out. After a two-hour flush the pressure was raised to 4238 kPa (600 psig) and the temperature was raised to about 135°C and maintained there for 12 hours. After the catalyst composite was cooled to 10°C, the feed blend was cut in and the regeneration gas stream was cut out. The entire procedure typically took 16-18 hours. A catalyst of aluminum chloride on gamma alumina extrudates containing 0.25 weight percent platinum was readily regenerated under the aforementioned conditions to afford an alkylate product of average RON of 90.5. Where butyl chloride was absent from the regeneration gas stream the catalyst initially showed very rapid deactivation and later was not regenerated to any measurable extent. This demonstrates the desirability, if not the necessity, of having butyl chloride present in the regeneration stream where liquid isobutane, as a representative hydrocarbon, is present along with hydrogen. Separate experiments showed that platinum could be replaced by either 0.5 weight percent palladium or nickel to afford catalysts regenerable under the same conditions as stated above. For both of the latter catalysts the product alkylate had an average RON of about 88.5. A catalyst of gallium chloride on gamma alumina extrudates containing 0.25 weight percent palladium also was readily regenerable under the stated conditions through at least 8 regenerations without any appreciable loss in activity or stability. Where regeneration was tried only with soluble hydrogen, i.e., hydrogen saturated in liquid isobutane, catalyst stability did deteriorate as evidenced by shorter process cycle times prior to the onset of deactivation. Catalysts prepared by subliming 1) zirconium tetrachloride, ZrCl 4 , on alumina containing 0.25 weight percent platinum, 2) titanium tetrachloride, TiCl 4 , on gamma alumina containing 0.25 weight percent platinum, and 3) aluminum chloride on spherical silica-alumina (75-90 weight percent silica) having 0.25 weight percent platinum were also shown to be regenerable over multiple process cycles. In all cases the product alkylate gave an average RON of 88-89. Catalysts were prepared of boron trifluoride, BF 3 , modified alumina with and without 0.25 weight percent platinum. Without platinum the catalyst was not regenerable, while with platinum the catalyst was regenerable for multiple cycles using either this procedure or that of Example 1. In all cases the product alkylate had an average RON of about 91.5.

Claims: A method of regenerating an at least partially deactivated solid catalyst comprising 1) the reaction product of a first metal halide and the bound surface hydroxyl groups of refractory inorganic oxide by treatment with hydrogen and recovering a regenerated catalyst having substantially increased alkylation activity characterized in that the catalyst is an alkylation catalyst containing said reaction product (1), and 2) a zerovalent second metal, wherein said first metal halide is a fluoride, chloride, or bromide and the first metal is selected from aluminum, zirconium, tin, tantalum, titanium, gallium, antimony, phosphorus, boron and mixtures thereof, and said zerovalent second metal is selected from platinum, palladium, nickel, ruthenium, rhodium, osmium, iridium, and mixtures thereof, said catalyst having become at least partially deactivated during its catalysis of the liquid phase alkylation of an alkene having from 2 to 6 carbon atoms with an alkane having from 4 to 6 carbon atoms, said method comprising removing substantially all of the liquid phase hydrocarbons from the catalyst, and treating the resulting catalyst with hydrogen in the presence of liquid isobutane and a chloride source at a partial pressure of 6.9 to 13790 kPa for a time from 1 to 20 hours at a temperature from 10 up to 300°C. A method according to Claim 1 characterized in that the first metal is selected from aluminum, zirconium, titanium, gallium, boron, and any combination thereof. A method according to Claim 1 or 2 characterized in that the second metal is platinum, palladium, or any combination thereof. A method according to any one of Claims 1 to 3 characterized in that the catalyst is treated with hydrogen at a temperature from 10 to 200°C. A method according to any one of Claims 1 to 4 characterized in that the chloride source is isobutyl chloride.

Inventors: KOCAL JOSEPH A, KOJIMA MASAMI, KOCAL, JOSEPH A., KOJIMA, MASAMI
Applicants: UOP INC, UOP
Application year: 1994
Main classification: B01J27
IPC codes: C07C2, B01J27